Process for preparation of isomers of 1-cyclohexyl-1,3,3-trimethylhydrindane

ABSTRACT

A process is disclosed for the hydrogenation of 1-phenyl-1,3,3trimethylindane to prepare selected isomers. For example 4,9-cis, 1-cyclohexyl-1,3,3-trimethylhydrindane, a fluid with improved tractive properties, can be prepared using a catalyst containing nickel, palladium or rhodium at a hydrogen pressure in the range of 600 to 1500 p.s.i.g., and a temperature substantially in the range of 200*C. to 225*C.

United States Patent [1 1 Hosler et al.

[ PROCESS FOR PREPARATION OF ISOMERS OF l-CYCLOHEXYL-l,3,3- TRIMETHYLHYDRINDANE [75} Inventors: Peter Hosler, Wallingford; David S.

Gates, Swarthmore, both of Pa.

[73] Assignee: Sun Research and Development Co.,

Philadelphia. Pa.

[22] Filed: Jan. 17, 1972 [2l] Appl. No.: 218,338

[52] U.S. Cl. 260/667 [51] Int. Cl. C07C 5/10 [58] Field of Search 260/667 [56] References Cited UNITED STATES PATENTS 2,629,751 2/l953 Wiggins 260/667 1 Dec. 30, 1975 3.411369 ll/l968 Hammann et al. 74/200 Primary Examiner-Veronica O'Keefe Attorney, Agent, or Firm-George L. Church; Donald R. Johnson; J. Edward Hess [57] ABSTRACT 12 Claims, 2 Drawing Figures U.S. Patent Dec. 30, 1975 Sheet20f2 3,929,923-

HYDROGENATION OF -METHYL STYRENE DIMER 250C I200 PSI H C isomer B isomer A isomer AMSD 02395200 om. u oz m0 .rzwommm HOURS FIGURE 2 PROCESS FOR PREPARATION OF ISOMERS OF 1-CYCLOHEXYL-1,3,3-TRIMETHYLHYDRIN- Serial No.

(Now U.S. 3.595.796 issued 7-27-71) 679.834 (Now US. 3.595.797 issued 7-27-71) 679.851 (Now US. 3.598.740. issued 8-10-71) 794.844 (Now U.S. 3.608.385. issued 9-28-71) 812.516 (Now US. 3,619,414. issued 11-9-71) 850.717 (now abandoned) 3.256 (Now U.S. 3.648.531 issued 3-14-72) 33.023 (Now abandoned) 78.191 (Now US. 3.676.521 issued 7-11-72) DANE CROSS REFERENCES TO RELATED APPLICATIONS The present application is related to the following listed applications:

Filing Date Title/lnventorts) Traction Drive Transmission Containing Naphthenes.

Branched Paraffins. or Blends of Naphthenes and Branched Paraffins as Lubricant IRL N. DULING and DAVID S. GATES Blending Branched Paraffin Fluids for Use in Traction Drive Transmission IRL N. DULlNG-DAVID S. GATES-MARCUS W. HASELTINE Traction Drive Transmission Containing Paraffinic Oil as Lubricant IRL N. DULING- DAVID S. GATES-THOMAS D. NEWINGHAM Friction Drive Fluid IRL N. DULING and FREDERICK P. GLAZIER Catalytic Hydrofinishing of Petroleum Distillates in the Lubricating Oil Boiling Range IVOR W. MILLS-MERRIT'I' C. KIRK. JR.- ALBERT T. OLENZAK Hydrorefined Lube Oil and Process of Manufacture lVOR W. MILLS and GLENN R. DIMELER Friction or Tractive Drive Fluid IRL N. DULING- FREDERlCK P. GLAZlER-DAVID S. GATES and ROBERT E. MOORE Combination of Tractive Drive and Traction Fluid Comprising Cyclic or Acyclic Compounds IRL N. DULING- FREDERICK P. GLAZIER Polyisobutylene Oil Having a High Viscosity Index GARY L. DRlSCOLL-IRL N. DULlNG-DAVID S. GATES Process of Preparing Synthetic Lubricants from Low Molecular Olefins RICHARD S. STEARNS-IRL N. DULING- DAVID S. GATES Synthetic Lubricants from Low Molecular Weight Olefins- RICHARD S. STEARNS-IRL. N. DULlNG-DAVID S. GATES Lubricant for Controlled- Slip Differential THOMAS D. NEWINGHAM-ALEXANDER D. PECCHUlTE-JOHN Q. GRIFFITH. Ill-MARCUS W. HASELTINE. JR. Blended Traction Fluid Containing Cyclic Compounds- IRL N. DULlNG-DAVID S. GATES Method for Improving the Coefficient of Traction Using Hydrogenated Polymeric Styrenes IRL N. DULlNG-DAVID S. GATES Blanched Olefin Polymers as Tractants IRL N. DULlNG-DAVID S. GATES C -C Naphthenes as Tractants IRL N. DULING- DAVID S. GATES Hydrorefined Naphthenic Oil as a Tractant DAVll) S. GATES-IRL N. DULING Blended Traction Fluid Containing Hydrogenated Polyolefin IRL N. DULING- DAVID S. GATES-FREDERICK P. GLAZlER-ROBERT E. MOORE- THOMAS D. NEWINGHAM BACKGROUND OF THE lNVENTlON The prior art described methods of preparation of l-cyclohexy-l.3.3-trimethylhydrindanc by the hydrogenation of l-phenyl-l.3.3-trimethylhydrindane. a dimer of alphamethylstyrene. However. the configurational isomers of the hydrogenated product have not been reported, nor have specific preparative methods for all of the isomers been disclosed.

Wiggins, U.S. Pat. No. 2.629.751. issued Feb. 24. 1953. has described the hydrogenation of l-phenyl- 1,3,3-trimethylindane at 300 p.s.i.g.. at temperatures beginning at 170C. and going to 325C. However, the Wiggins product appears to be mostly a low boiling isomer. with unattractive traction properties.

Hammann and Schisla. U.S. Pat. No. 3.41 L369. issued Nov. 19. 1968. teach that l-phenyll,3.3-trimethylindane can be hydrogenated at 2500 psig. starting at 90C. However. this product appears to be an intermediate boiling isomer. with less desirable traction properties than 4.9-cis. 1-cyc1ohexy1-l .3.3-trimethy1hydrindane.

BRIEF SUMMARY OF THE lNVENTlON The present application describes isomers of 1- cyclohcxyl-l.3.3-trimethy1hydrindane which have superior traction properties. and discloses methods for obtaining these isomers in high yield. The process of this invention can utilize a moderate pressure range suitable for large scale operation.

A process is disclosed for the hydrogenation of lphenyl-l.3.3-trimethylindane to prepare selected isomers. For example. 4.9-cis.l-cyclohexyl-l.3.3-trimethylhydrindane. a fluid with improved tractive properties. can be prepared using a catalyst containing nickel. palladium or rhodium at a hydrogen pressure in the range of 600 to 1500 psig. and a temperature substantially in the range of 200C to 225C.

The hydrogenation of l-phenyl-l.3.3-trimethylindane has been found to proceed in a series sequential reaction to compounds A. C and B in that order. Compounds A. B and C are predominant isomers of lcyclohexyl-l.3.3-trirnethylhydrindane. and characterized by the following physical properties (the prior art reports are also given for comparison):

Normal boiling point: calculated from Vapor Preuure Chart. J. B. Maxwell. Data Book on Hydrocarbonl. D. Van Noatrand. N.Y. 1950.

Compound C has the structure 4.9-cla-l'cyc|0hexyl-l.3.J-lrlmcthylhydrindune. while compound 8 la the 4.9-tran1tlromerv Catalytic hydrogenation of l-phenyl-l-3.3-trimcthylindane can be characterized by the following equation:

S-'i-- A-":--C-":-'B

where S is the starting material and A. B and C are the products described above.

The reaction rate constants. k are represented by the Arrhenius equation R==Ae RT where AH is the activation energy. T is temperature in K. and R is the gas constant. For the sequential reaction given above the energies of activation for the individual steps are found to be:

H, 7 10500 H, a 14.200 H, ,1 30.000 calories BRIEF DESCRIPTION OF THE DRAWINGS In the accompanying drawings. F108. 1 and 2 illustrate the influence of reaction time and temperature (at a given pressure and catalyst feed ratio) on isomer distribution and show how proper choice of reaction time and temperature can lead to improved (maximized) yields of a desired isomer or isomer mixture. FIG. 2 is similar to FIG. 1 except that the reaction temperature is at 250C. instead of 200C.

ILLUSTRATIVE EXAMPLES The following examples illustrate the manner in which the product isomer can be controlled by proper selection of conditions.

EXAMPLE 1 300 ml of molten l-phenyl-l .3.3-trimethylindane and 15 grams of 58% nickel on kieselguhr were charged to a one-liter stirred pressure reactor. After purging with hydrogen, the reactor was pressured to 1200 p.s.i. with hydrogen and held at that pressure for the course of the reaction. Heat was applied through electrical windings. with thermostatic controls to maintain 200C 10C. Samples were analyzed by UV spectroscopy and gas chromatography at 1. 2. 3 and 6 hours. to give the compositions indicated in FIG. I. At 6 hours. the reactor was cooled. the product withdrawn and the catalyst was removed by filtration. The viscosity of the resulting product was 38.21 cs at F. and 4.54 cs at 210F.

Example 2 A reactor was charged and operated in manner similar to Example 1. except that the temperature was controlled at 250C., with the results shown in FIG. 2. It is noted that product C has a maximum concentration at approximately 2 hours and then is gradually converted to product B.

Runs similar to those in Examples 1 and 2 are listed in the following table with the time for maximum C Example 3 A reactor was charged and operated in manner similar to Example 1, except Raney nickel was used as a catalyst, with the following results:

H, Pressure Products Temp., "C psi Time A B C 175 I200 6 70 l3 i7 200 1200 6 2 6 92 225 I200 6 2i 7 72 250 1200 6 20 I 64 in the experiments above with Raney nickel, the catalyst lost its activity at the higher temperatures, apparently because of the sintering of the nickel surface at high temperatures. The temperature range for this catalyst is narrowly limited to about 200C.

Example 4 Example A high pressure tubular flow reactor was charged with 4 liters (dry bulk volume) of58% nickel on kieselguhr pellets. The reactor was purged with nitrogen, then purged with hydrogen and pressured to i500 psi with hydrogen. Temperature in the reactor was maintaincd at 220C i 10C. l-phenyl-l,3,3-trimethylindane was diluted with 50% by volume cyclohexane and charged to the reactor at 350 ml/hour. After the reaction, the cyclohexane was removed by distillation and the resulting product was found to contain 3% product A, 7% produce 8, and 90% product C.

4,9-cisl -cyclohexyl-l ,3,3-trimethylhydrindane is especially useful as a component of a lubricant for a traction drive, roller clutch or limited slip differential,

particularly a lubricant comprising conventional nonhydrocarbon lube additives (e.g., extreme pressure, antioxidant, antirust, antifoam, antiwear, dispersant) and a hydrocarbon base containing the hydrindane and 0.1-20 parts (based on the hydrindane) of a hydrogenatcd linear, liquid polymer of isobutylene.

The invention claimed is:

l. A process for the hydrogenation of l-phenyll ,3,3- trimethylindane comprising contacting said indane or a feed consisting essentially of said indane with hydrogen and with a hydrogenation catalyst containing nickel, palladium or rhodium, at a hydrogen pressure in the range of 600 to i500 psig and a temperature in the range of 200 to 225C, and recovering a product of said contacting which consists essentially of perhydrogenated l-phenyl-l ,3,3-trimethylindane and including a major proportion of 4,9-cis-l-cyclohexyl-l,3,3- trimethyl hydrindane.

2. Process according to claim 1 wherein at least of the product of said hydrogenation is 4,9-cis-leyclohexyl-l ,3 ,B-trimethylhydrindane.

3. Process according to claim 2 wherein said catalyst consists essentially of nickel on an inert carrier.

4. Process according to claim 3 wherein said inert carrier is kieselguhr and said pressure is in the range of lOO0-l500 p.s.i.

5. Process according to claim I wherein said catalyst comprises about 58% nickel on kieselguhr.

6. Process according to claim 1 wherein said contacting is for sufficient time to maximize production of 4,9-cis, l -cyclohexyl-l ,3 ,3-trimethylhydrindane and minimize production of other isomers of hydrogenated l-phenyl-l ,3,3-trimethylindane.

7. Process according to claim 6 wherein said catalyst consists essentially of about 58% nickel on kieselguhr.

8. Process according to claim 7 wherein said contacting is at 220C. 10C.

9. Process according to claim 8 wherein said pressure is about 1500 psi.

10. Process according to claim 1 wherein said products have a normal boiling point of at least 578F and a refractive index at 20C of less than l.5055.

11. Process according to claim 1 wherein said catalyst consists essentially of nickel, palladium or rhodium.

12. Process according to claim 1 wherein a major proportion of the product of said contacting boils at about 613F. 

1. A PROCESS FOR THE HYDROGENATION OF 1-PHENYL1,3,3TRIMETHYLINDANE COMPRISING CONTACTING SAID INDANE OR A FEED CONSISTING ESSENTIALLY OF SAID INDANE WITH HYDROGEN AND WITH A HYDROGENATION CATALYST CONTAINING NICKEL, PALLADIUM OR RHODIUM, AT A HYDROGEN PRESSURE IN THE RANGE OF 600 TO 1500 PSIG AND A TEMPERATURE IN THE RANGE OF 200* TO 225*C, AND RE COVERING A PRODUCT OF SAID CONTACTING WHICH CONSISTS ESSENTIALLY OF PERHYDROGENATED 1-PHENYL-1,3,3-TRIMETHYLINDANE AND INCLUDING A MAJOR PROPORTION OF 4,9-CIS-1-CYCLOHEXYL1,3,3-TRIMETHYL HYDRINDANE.
 2. Process according to claim 1 wherein at least 80% of the product of said hydrogenation is 4,9-cis-1-cyclohexyl-1,3,3-trimethylhydrindane.
 3. Process according to claim 2 wherein said catalyst consists essentially of nickel on an inert carrier.
 4. Process according to claim 3 wherein said inert carrier is kieselguhr and said pressure is in the range of 1000-1500 p.s.i.
 5. Process according to claim 1 wherein said catalyst comprises about 58% nickel on kieselguhr.
 6. Process according to claim 1 wherein said contacting is for sufficient time to maximize production of 4,9-cis,1-cyclohexyl-1, 3,3-trimethylhydrindane and minimize production of other isomers of hydrogenated 1-phenyl-1,3,3-trimethylindane.
 7. Process according to claim 6 wherein said catalyst consists essentially of about 58% nickel on kieselguhr.
 8. Process according to claim 7 wherein said contacting is at 220*C. + or - 10*C.
 9. Process according to claim 8 wherein said pressure is about 1500 psi.
 10. Process according to claim 1 wherein said products have a normal boiling point of at least 578*F and a refractive index at 20*C of less than 1.5055.
 11. Process according to claim 1 wherein said catalyst consists essentially of nickel, palladium or rhodium.
 12. Process according to claim 1 wherein a major proportion of the product of said contacting boils at about 613*F. 